Production of petrol



PRODUCTION OF PETROL Filed March 28, 192?.`

GI asolime ProduC'S d. *4 1 Condenser 41m" --Gasolwxe V- Vapor Franciao-TL. q Colum r1 Ds'killae (AH or Parijs) Eesndmmn Y Su erheczn or Crckmci Chamber Pump 'Cvude Zzv/v ce1-afan I. Tui/kel,

Awal

ratentea'Apr. 28,1925.

FRANK TINKER, 'or EnnINGToN, BIRMINGHAM, ENGLAND.

rRoDUoTroN or PETROL.

\ .i Application filed March 2S, 1922. Serial No. 547,474.

To all 'whom i may concern.'

Be it known that I, FRANK TINKnn, a .sub-

ject of the King of Great Britain, residing at Erdingtom in the fcity ofBirmingham,

England, haveqinvented certain new and useful Improvements Relatinvr tothe Production of Petrol, of which th specification. p p c In theyspecification of a former United `St-atesfLetter-s Patent No.1,393,184, granted to me, I have described a process for-the productionof petrol (or gasoline)` from crude mineral oils by means compr1s1ng a Ystill, a superheating or'cracking chamber,

land a fractionating column.

In the said process supcrheated vapounfromthe cracking ychamber wasmixed wlth a stream of crude oil', and the'mixture was delivered to thefractionating column, andthe whole of the residuecollecting at the baseof the fraetionating'columnwas returned to the still for partialconversion into superheated va our. I i

.EVhen dealing with some crude 011s, particularly those containing.asphaltio compounds .and sulphur, I nd it undesirable to return to thestill the whole-'of the residue after treatment' of the crude oil withsuper` heated vapour, and the object of this invention is to enable theheavier constituents,-

which ordinarily contain impurities, to be tlon.

heated crudeoil is mixed with superheated oil vapour in a mixingchamber; the intermingled products are then passed to a` separating'`chamber where the heayy residues are collected and removed,`the vapourspassing on to a fractionatingcolumn; condensate Y from the lower "partofthis column is withdrawn tothe still and super/heater for pro-'.-

ductionof the superheated vapour re uired for admixture with the crudeoil,`and t e uncondensed vapour is passed on to a condenser.

The accompanying drawing illustrates l diagramma-tically one mode ofcarrying the invention into elfect. Referring to the diagram, Icombinationa still a; a superheater or vcracking chamber b, 'a mixingchamber c, and a fractionating column el. A separatingchamber eisa-rrangedbetweenA the mixing chamber 'and the iractionating column. Thesuperheated vapour and crude oil. are brought together at Athe upperend. of the e following is a emoved from the system before fractiona-According to .the present` invention preemploy in ymixing chamber c, andthe lower end of the separating chambere is provided with a pipe j bywhich residue collecting in the said f chamber can be drainedcontinuously from the system. The various parts are connected bypipes asshown.

For preheating the crude oil I may employ ay variety of methods. 'Ihuse. g. the residue from the chamber e may be passed through onecompartment of the heat interchanger f for imparting its heat tothe derthe actionof-,a pump g the crude oil is crude oil. AUnforced through theother compartment of the heat interchanger f, to a fire-heated pipesystem It where its temperature is further raised. Both'these heatingdevices may be supplemented by others in which the heat of vapoursdelivered by the system is utilized. l

Any. of these methods maybe used singly or in combination. I find inpractice that due, and subsequent heating by ireis convenient. In thepreheating operationthe crude oil vdelivered into c is raisedto such atemipreheating bylheat obtained from the resiperatu're that the heat ofthe superheated vapour from b can be used for evaporating the lighter.and medium fractions from the crude oil. "A greater volume of distillateis thus taken from the crude oil thanwould be -obtained if all theheating were effectedby the superheated vapour, and distillates l onlypass on from the mixingfchamberc and vthe chamber eto the fractionatingcolumn d. In the latter the vapours are fractionally condensed in such away as to return to the stillerl suilicient oil to provide the il:lrequired superheated vapour.A As' above stated the heavy residues aredrawn out of the system at the part le' and condensates only arecollected -in d. Vapours not lcollected in d pass to a condenser z' and'after condensation are withdrawn.

I claim :v

, l. In the production of low boiling point' hydrocarbons from highboiling point hydrocarbons, the process comprising mixing superheated'hydrocarbon vapors with a main stream of preheated crudehydrocarbon inla mixing chamber, passing the mix-A turevin a restricted stream througha pipe td an enlarged drum, drawing off a part, at- I' 'I least, of thecondensate from said d-rumandpassingthe vapors into a fractionatingcolumn,`.del1vering the condensate `from the vfractionating column intoa still, generating -r Y. vapors in the 'still and superheating thestill l vapors in thesup'erheatingdevice for subsequent mixture withlthe main stream ofv I' i hydrocarbons from high boiling pointhydrocarbons, the process which consists in mixing superheatedhydrocarbon vapors with a'main stream of preheated 'crude hydrocarbonsin a mixing chamber, passing the mixture' in a restricted stream througha pipe to an enlarged drum, drawinggat least, -apart of the condensatefrom said drum and passing'it through a heat eX- changer topreheat thestream of crude hydrocarbons, passing the vapors from the separatingdrum into a fraotionating'-column and delivering the condensate from thelatter into a-still, generating vapors in .the still, and superheatingthe stillvapors in the super-heating device for subsequent mixture withthe main stream of preheated crude hydrocarbons in a continuous process.

lIn testimony'iwhereof I have signed my name to this specification.

FRA'K TINKER.

